Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/40—Regeneration or reactivation
  • B01J31/4015—Regeneration or reactivation of catalysts containing metals
  • B01J31/4023—Regeneration or reactivation of catalysts containing metals containing iron group metals, noble metals or copper
  • B01J31/4038—Regeneration or reactivation of catalysts containing metals containing iron group metals, noble metals or copper containing noble metals
  • B01J31/4046—Regeneration or reactivation of catalysts containing metals containing iron group metals, noble metals or copper containing noble metals containing rhodium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/40—Regeneration or reactivation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
  • B01J31/20—Carbonyls
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
  • B01J31/24—Phosphines, i.e. phosphorus bonded to only carbon atoms, or to both carbon and hydrogen atoms, including e.g. sp2-hybridised phosphorus compounds such as phosphabenzene, phosphole or anionic phospholide ligands
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
  • B01J31/24—Phosphines, i.e. phosphorus bonded to only carbon atoms, or to both carbon and hydrogen atoms, including e.g. sp2-hybridised phosphorus compounds such as phosphabenzene, phosphole or anionic phospholide ligands
  • B01J31/2404—Cyclic ligands, including e.g. non-condensed polycyclic ligands, the phosphine-P atom being a ring member or a substituent on the ring
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J38/00—Regeneration or reactivation of catalysts, in general
  • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
  • B01J38/12—Treating with free oxygen-containing gas
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
  • C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
  • C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C47/00—Compounds having —CHO groups
  • C07C47/02—Saturated compounds having —CHO groups bound to acyclic carbon atoms or to hydrogen
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
  • C07F9/02—Phosphorus compounds
  • C07F9/28—Phosphorus compounds with one or more P—C bonds
  • C07F9/50—Organo-phosphines
  • C07F9/53—Organo-phosphine oxides; Organo-phosphine thioxides
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
  • B01J2231/30—Addition reactions at carbon centres, i.e. to either C-C or C-X multiple bonds
  • B01J2231/32—Addition reactions to C=C or C-C triple bonds
  • B01J2231/321—Hydroformylation, metalformylation, carbonylation or hydroaminomethylation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
  • B01J2531/82—Metals of the platinum group
  • B01J2531/822—Rhodium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
  • B01J31/18—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes containing nitrogen, phosphorus, arsenic or antimony as complexing atoms, e.g. in pyridine ligands, or in resonance therewith, e.g. in isocyanide ligands C=N-R or as complexed central atoms
  • B01J31/1845—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes containing nitrogen, phosphorus, arsenic or antimony as complexing atoms, e.g. in pyridine ligands, or in resonance therewith, e.g. in isocyanide ligands C=N-R or as complexed central atoms the ligands containing phosphorus
  • B01J31/1875—Phosphinites (R2P(OR), their isomeric phosphine oxides (R3P=O) and RO-substitution derivatives thereof)
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/50—Improvements relating to the production of bulk chemicals
  • Y02P20/584—Recycling of catalysts

Definitions

• This invention relates to a process for selectively converting alkyl substituted phosphine present in a hydroformylation reaction medium to its corresponding phosphine oxide, while at the same time improving the activity of the rhodium complex hydroformylation catalyst contained in said medium.
• the rhodium complex catalyst loses activity (i.e. becomes partially deactivated) during prolonged use and thus reactivation of such partially deactivated catalysts is of extreme importance to the state of the art due to the high cost of rhodium values. While it is difficult to ascertain all of the reasons for such an activity loss it is believed that in large scale hydroformylation reactions that the loss in activity is due at least in part to the presence of alkyl substituted phosphine in the hydroformylation medium. For instance it is known that the presence of alkyldiarylphosphine in the rhodium complex catalyzed hydroformylation of the alpha-olefin, propylene, inhibits catalyst productivity, i.e.
• alkyldiarylphosphine when triarylphosphine ligand is employed in the hydroformylation of an alpha-olefin, alkyldiarylphosphine is produced in situ, the "alkyl" group thereof normally being derived from the alpha-olefin undergoing hydroformylation and the "aryl” groups thereof being the same as the aryl of the triarylphosphine and that in a continuous hydroformylation reaction of alpha-olefins in the presence of triarylphosphine ligand to produce aldehydes, the continued build-up of such alkyl substituted phosphines can eventually lead to an unacceptable decrease in the rate of reaction and activity of the rhodium complex catalyst due to the affinity of such alkyl substituted phosphines for the catalyst.
• U.S. Pat. No. 3,555,098 relates to maintaining or improving the rhodium catalytic activity of a hydroformylation reaction by washing all or a portion of a liquid medium containing the catalyst with an aqueous solution, e.g. an aqueous alkaline solution, to remove by-product acid, e.g. carboxylic acid, formed during hydroformylation by oxidation of the aldehyde which may have been due to oxygen contamination of the reactant gas stream.
• an aqueous solution e.g. an aqueous alkaline solution
• Japanese Patent Application Publication No. 23,212/76 relates to maintaining or improving the rhodium catalytic activity of a hydroformylation reaction by removing the aldehyde from the distilled reaction product mixture containing the catalyst and then treating all or a portion of the liquid catalyst medium with oxygen during the recycling procedure of the catalyst back to the hydroformylation reaction.
• U.S. Pat. No. 4,196,096 relates to a method for regenerating rhodium hydroformylation catalysts which comprises the steps of removing all or a portion of the inactive catalyst from the hydroformylation reaction, adjusting the aldehyde content so as to have at least one mole of aldehyde per mole of rhodium and ligand (e.g. triphenylphosphine) present and treating the aldehyde containing catalyst with oxygen or an oxygen containing gas at a temperature less than the boiling point of the aldehyde, removing any solid material formed during oxidation and adjusting the ligand to rhodium ratio as required for use in the hydroformylation reaction.
• ligand e.g. triphenylphosphine
• U.S. Pat. No. 4,221,743 relates to a hydroformylation process wherein the rate of productivity of the process can be maintained at a desired rate by feeding a sufficient amount of oxygen during the hydroformylation reaction to the homogeneous liquid phase composition of the reaction so as to maintain or increase the activity of the rhodium catalyst.
• the generic aspect of this invention can be described as a process for converting alkyl substituted phosphine by-product to its corresponding phosphine oxide and improving the activity of a rhodium complex hydroformylation catalyst contained in a hydroformylation reaction medium, which catalyst has become partially deactivated from its employment in a continuous hydroformylation reaction to produce aldehyde products by reacting an olefinic compound, carbon monoxide and hydrogen in the presence of a hydroformylation reaction medium contained in a reaction vessel, said process comprising stopping the hydroformylation reaction being conducted in said vessel and treating, under non-hydroformylation conditions, all or a proportionate part of the hydroformylation reaction medium derived therefrom which consists essentially of from about 5 to about 60 percent by weight of aldehyde products, from about 10 to about 70 percent by weight of higher boiling aldehyde condensation by-products, a partially deactivated soluble rhodium complex hydroformylation catalyst in an amount sufficient to provide
• hydroformylation reaction mediums to be treated according to this invention may be derived from any suitable continuous hydroformylation process
• the preferred hydroformylation reaction mediums employable in the present invention are those hydroformylation reaction mediums derived from the continuous hydroformylation procedures taught in said U.S. Pat. No. 4,148,830 and said U.S. patent application Ser. No.
• the hydroformylation reaction mediums of such reactions still retain a substantial amount of aldehyde products during the reaction, the amount of which can be governed by the feed of the olefinic compound, hydrogen and carbon monoxide and other reaction conditions as explained in said U.S. Pat. No. 4,148,830 and said Ser. No. 776,934, and which may range from about 5 percent to about 60 percent by weight of said aldehyde products based on the total weight of said hydroformylation reaction medium.
• aldehyde products that are present in the hydroformylation reaction medium to be treated according to this invention will obviously correspond to those aldehyde products produced by the particular continuous hydroformylation reaction from whence said medium to be treated is derived.
• aldehyde products are mixtures rich in their normal to isomer ratio, i.e., contain at least about four moles of normal aldehyde product per mole of isomeric aldehyde product.
• the continuous hydroformylation of propylene produces butyraldehyde products, which products under preferred operational conditions are rich in their normal to isomer ratio.
• aldehyde products contained in a given hydroformylation reaction medium to be treated according to this invention will depend upon the particular olefinic compound employed in the continuous hydroformylation reaction from whence said medium to be treated is derived.
• Said aldehyde products each contain one more carbon atom than the olefinic compound employed in the hydroformylation reaction.
• Olefinic compounds that may be employed in such hydroformylation reactions include those containing from 2 to 20 carbon atoms and which may contain groups or substituents that do not essentially interfere with the course of the hydroformylation reaction and the process of this invention, such as generically taught in the prior art, especially U.S. Pat. No. 3,527,809.
• Illustrative olefinic compounds include alkenes such as alpha olefins and internal olefins, alkyl alkenoates, alkenyl alkanoates, alkenyl alkylethers, alkenols, and the like.
• the preferred olefinic compounds are alpha-olefins containing from 2 to 20 carbon atoms and more preferably from 2 to 6 carbon atoms, such as ethylene, propylene, 1-butylene, 1-pentylene, 1-hexylene, and the like.
• the process of this invention is especially useful for treating a hydroformylation reaction medium derived from the continuous hydroformylation of propylene to form butyraldehydes having a high normal to isomer ratio, as disclosed in said Ser. No. 776,934.
• the amount of aldehyde products contained in the hydroformylation reaction medium to be treated according to this invention will also be dependent upon the particular continuous hydroformylation reaction employed from whence said medium to be treated is derived and may range from about 5 percent to about 60 percent by weight based on the total weight of said derived medium, more preferably said derived medium contains from about 10 to about 30 percent by weight of aldehyde products based on the total weight of said derived medium.
• Such may be accomplished by any suitable method such as by sufficiently lowering the temperature and pressure of the reaction vessel while maintaining its cycle flow, so as to remove mainly only the desired amount of excess aldehyde products and to minimize the loss of any of the other components contained in the hydroformylation reaction medium. While the purpose of removing excess aldehyde product is largely economical, i.e., the recovery of additional desired aldehyde product, its removal also serves the purpose of minimizing the amount of carboxylic acid that may be formed during the oxidation treatment of this invention, as well as being an oxidative safety consideration that is recommended herein.
• the free alkyl substituted phosphine by-product i.e. that amount alkyl substituted phosphine by-product that is not complexed with or tied to the rhodium complex hydroformylation catalyst
• the free alkyl substituted phosphine by-product present in the hydroformylation reaction medium to be treated according to this invention, and which can be selectively converted to its corresponding phosphine oxide by this invention, may be any phosphine of the type shown by Formula I above.
• alkyl substituted phosphine by-product such as shown by Formula I above
• some alkyl substituted phosphine by-product such as shown by Formula I above
• the "alkyl" group(s) thereof normally being derived from the olefinic compound undergoing hydroformylation
• the "aryl" group(s) thereof normally corresponding to the aryl radical of the triarylphosphine ligand.
• alkyl substituted phosphine by-product present in the hydroformylation reaction mediums to be treated according to this invention may consist of mixtures of one or more such alkyl substituted phosphines.
• Dialkylarylphosphines which may also possibly be present as a result of in situ formation can also be converted to their corresponding phosphine oxides by the process of this invention.
• the alkyl radical of said alkyl substituted phosphine may be any alkyl radical containing from 2 to 20 carbon atoms and may be straight or branched-chained and may contain groups or substituents which do not essentially interfere with the process of this invention. Note however, that it is not applicants' intention to be bound by any precise discussion or explanation of how said alkyl substituted phosphines are formed in situ, it being sufficient for the purpose of this invention to simply point out that their in situ formation is possible and that such alkyl substituted phosphines can be converted to their corresponding oxides when present in the hydroformylation reaction medium by the oxidative treatment of said medium according to this invention.
• the particular free alkyl substituted phosphine by-product, as well as its amount, present in a given hydroformylation reaction medium to be treated according to this invention will obviously correspond to and merely be dependent upon the particular alkyl substituted phosphine by-product that has been formed in situ and the amount accumulated in the particular hydroformylation reaction medium from whence the hydroformylation reaction medium to be treated according to this invention has been derived.
• the amount of free alkyl substituted phosphine by-product present in the hydroformylation medium to be treated according to this invention may range from 0.1 to about 5 percent by weight and more preferably ranges from about 0.2 to about 2.5 percent by weight, based on the total weight of said medium.
• the free triarylphosphine ligand i.e. that amount triarylphosphine that is not complexed with or tied to the rhodium complex hydroformylation catalyst
• the free triarylphosphine ligand can be any triarylphosphine ligand suitable for use in continuous hydroformylation reactions, such as taught by said U.S. Pat. Nos. 3,527,809 and 4,148,830 and said Ser. No. 776,934.
• Illustrative triarylphosphine ligands include triphenylphosphine, trinaphthylphosphine, tritolylphosphine, tri(p-biphenyl) phosphine, tri(p-methoxyphenyl) phosphine, p-(N,N-dimethylamino)phenyl diphenylphosphine, and the like.
• the amount of free triarylphosphine ligand present in the hydroformylation reaction medium to be treated according to this invention may range from about 5 percent by weight to about 25 percent by weight, preferably from about 8 percent by weight to about 15 percent by weight, based on the total weight of said medium to be treated.
• particularly advantageous results are achieved when the amount of free triarylphosphine ligand in the hydroformylation reaction medium of such reactions is at least about 100 moles of free triarylphosphine per mole of catalytically active rhodium metal present in the rhodium complex hydroformylation catalyst.
• the preferred hydroformylation reaction medium to be treated according to this invention will also generally contain at least about 100 moles of free triarylphosphine ligand per mole of catalytically active rhodium metal present in the rhodium complex hydroformylation catalyst of said hydroformylation reaction medium to be treated according to this invention.
• the partially deactivated rhodium complex hydroformylation catalyst, present in the hydroformylation reaction medium to be treated according to this invention can be any rhodium hydroformylation catalyst suitable for use in continuous hydroformylation reactions, such as taught by said U.S. Pat. Nos. 3,527,809 and 4,148,830 and said Ser. No. 776,934, and which has been employed in the continuous hydroformylation reaction to the extent that it has become partially deactivated i.e. does not have the same rate of activity of corresponding fresh rhodium complex catalyst.
• the preferred hydroformylation reaction mediums contain a rhodium complex catalyst consisting essentially of rhodium complexed with carbon monoxide and triarylphosphine (corresponding to the free triarylphosphine ligand also contained in said medium).
• a rhodium complex catalyst consisting essentially of rhodium complexed with carbon monoxide and triarylphosphine (corresponding to the free triarylphosphine ligand also contained in said medium).
• alkyl substituted phosphine of formula (I) above is formed in situ, the amount of which continues to build up over the period of time that the continuous hydroformylation reaction is operational.
• Said alkyl substituted phosphine ligand having a greater affinity for rhodium than triarylphosphine may also tie or bind itself to the rhodium thereby resulting in a rhodium complex catalyst consisting essentially of rhodium complexed with carbon monoxide, triarylphosphine ligand and/or said alkyl substituted phosphine ligand (i.e. either one or both of said triarylphosphine ligand and said alkyl substituted phosphine ligand).
• rhodium complex catalyst terminology “consisting essentially of”, as employed herein, is not meant to exclude, but rather include the likely possibility of alkyl substituted phosphine and hydrogen complexed with the rhodium in addition to carbon monoxide and triarylphosphine, the hydrogen being derived from the hydrogen gas of the hydroformylation reaction if not already present in the catalyst precursor.
• rhodium complex hydroformylation complex catalyst may be formed in situ during the hydroformylation reaction or preformed by methods known in the art.
• preformed rhodium hydridocarbonyl-tris triphenylphosphine
• rhodium hydridocarbonyl-tris triphenylphosphine
• rhodium catalyst precursors such as rhodium carbonyl triphenylphosphine acetylacetonate, Rh 2 O 3 , Rh 4 (CO) 12 , Rh 6 (CO) 16 , Rh(NO 3 ) 3 or rhodium dicarbonyl acetylacetonate, and the like, may be introduced into the reaction medium of the hydroformylation reaction.
• an active rhodium complex hydroformylation catalyst is formed in the hydroformylation reaction medium under the conditions of hydroformylation wherein said alkyl substituted phosphine by-product is also formed in situ.
• carbon monoxide, triphenylphosphine, hydrogen and said alkyl substituted phosphine by-product are all ligands that are capable of being complexed with the active rhodium complex catalyst of the continuous hydroformylation reaction employed herein.
• the amount of partially deactivated rhodium complex hydroformylation catalyst present in the hydroformylation reaction medium to be treated according to this invention will correspond to that catalytic amount of catalyst present in the continuous hydroformylation reaction from whence said medium to be treated has been derived, and may be that amount sufficient to provide a rhodium concentration in said medium to be treated which may range from about 25 ppm to about 1200 ppm and preferably from about 50 ppm to about 400 ppm of rhodium calculated as free metal.
• the particular higher boiling aldehyde condensation by-products, as well as their amount, present in a given hydroformylation reaction medium to be treated according to this invention will obviously correspond to and merely be dependent upon the particular higher boiling aldehyde condensation by-products formed in situ and the amount accumulated in the particular hydroformylation reaction medium from whence the hydroformylation medium to be treated according to this invention has been derived.
• the amount of higher boiling aldehyde condensation by-products present in the hydroformylation medium to be treated according to this invention may range from about 10 to about 70 percent by weight and more preferably ranges from about 25 to about 60 percent by weight, based on the total weight of said medium.
• this invention comprises stopping a continuous hydroformylation reaction being conducted in a reaction vessel and treating, under non-hydroformylation conditions, the hydroformylation reaction medium derived therefrom with oxygen or an oxygen containing gas until at least 25 percent by weight of the alkyl substituted phosphine by-product present in said derived medium has been converted to its alkyl substituted phosphine oxide, while at the same time converting less than about 50 percent by weight of the triarylphosphine ligand present in said derived medium to its triarylphosphine oxide.
• the hydroformylation reaction can obviously be stopped by any convenient method, such as by stopping the feed of olefinic compound, carbon monoxide and hydrogen, to the reaction vessel, allowing the residual reactants contained therein to react to completion, and shutting down the reaction being conducted in the reaction vessel.
• the recycle lines of the continuous reaction system can then be cleared in any conventional manner and the derived hydroformylation medium treated with oxygen or an oxygen containing gas as taught herein.
• the oxidative treatment of this invention which is conducted, under non-hydroformylation conditions, i.e. while the hydroformylation reaction has been stopped as explained above, may be accomplished by adding oxygen or an oxygen containing gas to all or a proportionate part of the derived hydroformylation reaction medium in any manner which seems most convenient and suitable.
• the method of treating the hydroformylation medium is not critical and can be accomplished simply by adding a sufficient amounts of oxygen for a sufficient period of time to obtain the desired result.
• the oxygen or oxygen containing gas can be fed directly to and thoroughly dispersed through the hydroformylation medium while it is contained in the hydroformylation reaction vessel by introducing it into the recycle lines of the continuous hydroformylation reaction system and pumping same into said medium.
• the hydroformylation reaction medium to be treated can be removed from the reactor and treated in a separate vessel.
• the use of sufficient oxygen or an oxygen containing gas for a sufficient period of time to convert at least about 25 percent by weight, preferably at least about 50 percent by weight of the alkyl substituted phosphine to its oxide while at the same time converting less than about 50 percent by weight, preferably less than about 25 percent by weight of the triarylphosphine ligand to its oxide should be sufficient to provide satisfactory improvement in the activity of the partially deactivated catalyst.
• the amounts of alkyl substituted phosphine and triarylphosphine ligand converted to their oxides may be easily monitored by any conventional analytical method such as gas chromatography.
• the improved activity of the hydroformylation reaction medium so treated according to this invention may be determined by measuring the rate of reaction obtained upon employing said hydroformylation reaction medium against the rate of reaction of a similar hydroformylation reaction medium using fresh catalyst in the same manner. Of course one may also merely compare the activity of the hydroformylation medium immediately before and after it has been treated according to this invention. The difference in hydroformylation rates (or difference in catalyst activity) may then be observed in a convenient laboratory time frame such as in terms of gram-moles per liter-hour of aldehyde product produced.
• oxygen it is to be understood that oxygen need not be employed in its pure form, but more preferably and conveniently is employed in the form of an oxygen containing gas, such as air or in admixtured with an inert gas such as nitrogen in order to minimize any explosive hazards. Indeed while oxygen in the form of air is most convenient, it too may be diluted with an inert gas such as nitrogen in order to reduce its oxygen content to provide safer operating conditions when warranted. Thus it should be fully understood that when employing this invention one must be careful to avoid those conditions which could lead to the possibility of explosive detonation occurring by virtue of a large concentration of oxygen in a confined space.
• the oxygen treatment encompassed herein is designed to convert at least about 25 percent by weight of the free alkyl substituted phosphine by-product to its phosphine oxide, but less than 50 percent by weight of the free triarylphosphine ligand to its phosphine oxide in the hydroformylation reaction medium and thereby obtain a desired improvement in the activity of the rhodium complex catalyst that has become at least partially deactivated over that obtained in the absence of such an oxygen treatment and because the components least partially deactivated over that obtained in the of the hydroformylation reaction medium can vary both in terms of their nature and concentrations, it is apparent no specific values can be arbitrarily given to conditions such as the amount and partial pressure (concentration of oxygen), temperature, and contact time for the oxygen treatment.
• Such conditions which may vary greatly, are not narrowly critical and obviously need only to be at least sufficient to obtain the results desired. Thus in some cases a small amount of oxygen may be more beneficial, while in other circumstances a large amount of oxygen may prove more desirable. For example, while only a small amount of oxygen may be needed in a given circumstance, it may be more desirable to use a higher concentration, and therefore a larger amount of oxygen, in order to reduce contact time. Accordingly, treatment conditions such as temperature, partial pressure (concentration) and contact time will also vary greatly and any suitable combination of such conditions may be employed herein. For instance, a decrease in any one of such conditions may be compensated for by an increase in one or both of the other conditions, while the opposite correlation is also true.
• the oxygen may be added to the hydroformylation medium at liquid temperatures ranging from about 20° C. to about 80° C. while temperatures ranging from about 25° C. to about 60° C. should be suitable in most instances. Moreover oxygen partial pressures ranging from as little as 10 -4 to 10 atmospheres should be sufficient for most purposes.
• the contact time will be directly related to such conditions as temperature and oxygen concentration and may vary from a matter of seconds or minutes to hours.
• the subject oxygen treatment of this invention is unique in that it has been surprisingly discovered that the hydroformylation reaction medium of a continuous hydroformylation reaction can be treated all at one time and in the same reaction vessel of said reaction under mild conditions after stopping the reaction so as to selectively convert undesirable free alkyl substituted phosphine to its non-detrimental corresponding oxide despite the concurrent presence of the large excess of aldehyde product and triarylphosphine ligand also contained in said medium, and thereby improve the rate of activity of the rhodium complex catalyst that has become at least partially deactivated from said continuous reaction.
• the subject invention furnishes one with a much wider processing latitude with regard to controlling safety considerations and in balancing the degree of improvement obtained in catalyst reactivity against the possible large loss of costly desirable components such as aldehyde product and triarylphosphine ligand as a result of their conversion to carboxylic acid and triarylphosphine oxide that may be attendant with a process such as disclosed in said U.S. Pat. No. 4,221,743 which requires its oxidative treatment to be conducted during the actual operation of the hydroformylation reaction.
• the subject inventive process is further unique in that since the oxidation treatment of this invention can be carried out in the same reaction vessel of the hydroformylation reaction one need only turn back on the feed of olefinic compound, hydrogen and carbon monoxide to the treated hydroformylation reaction medium of this invention and restart the continuous hydroformylation reaction without the need of adding additional reaction medium components before restarting the reaction.
• the enhanced activity of the rhodium complex catalyst obtained by the subject oxygen treatment of this invention is a sustained improvement that is not drastically reversible upon immediate use of the catalyst, but which is self-maintaining for long periods of time.
• a hydroformylation reaction medium was obtained from a continuous gaseous hydroformylation reaction of propylene to produce butyraldehyde, said reaction comprising feeding propylene, carbon monoxide and hydrogen to a reaction vessel and reacting same in the presence of a hydroformylation reaction medium contained therein comprising butyraldehyde products, higher boiling aldehyde condensation by-products as the solvent, free propyldiphenylphosphine, free triphenylphosphine, and a soluble rhodium complex hydroformylation catalyst consisting essentially of rhodium complexed with carbon monoxide and triphenylphosphine, said medium containing about 387 ppm rhodium (calculated as free metal) and whose catalytic activity had declined to about 30 percent of that of fresh catalyst, by shutting off the reactant feed gases, stopping the hydroformylation reaction and stripping essentially all (more than 99.5%) of said reactant gases from the reaction vessel and cycle lines.
• hydroformylation reaction medium so obtained showed it to contain about 14 percent by weight of butyraldehyde products, about 63 percent by weight of higher boiling aldehyde condensation by-products, about 0.9 percent by weight of free propyldiphenylphosphine, and about 17 percent by weight of free triphenylphosphine, the remainder consisting essentially of said rhodium complex catalyst, triphenylphosphine oxide and higher boiling organic components, e.g. aldehyde pentamers.
• Said derived hydroformylation reaction medium was then oxygenated while present in the same reaction vessel by passing a gaseous air-nitrogen mixture (about 4% oxygen) through said medium for about 14 hours, at about 70° C., about 58 p.s.i.g., and at an average feed flow rate of about 10.1 standard cubic feet of gas per hour per gallon of said derived medium to obtain an oxygenated treated hydroformylation reaction medium containing about 8 percent by weight of butyraldehyde products, about 0.05 percent by weight of free propyldiphenylphosphine and about 13 percent by weight of free triphenylphosphine, in addition to the other components mentioned above and present in said medium before said oxygen treatment.
• a gaseous air-nitrogen mixture about 4% oxygen
• Said analysis indicates that about 94 percent by weight of the original free propyldiphenylphosphine was oxidized to its corresponding phosphine oxide while only about 23 percent by weight of the original free triphenylphosphine was oxidized to its corresponding phosphine oxide by said oxygen treatment.
• a hydroformylation reaction medium was obtained from a continuous gaseous hydroformylation reaction of propylene to produce butyraldehyde, said reaction comprising feeding propylene, carbon monoxide and hydrogen to a reaction vessel and reacting same in the presence of a hydroformylation reaction medium contained therein comprising butyraldehyde products, higher boiling aldehyde condensation by-products as the solvent, free propyldiphenylphosphine, free triphenylphosphine, and a soluble rhodium complex hydroformylation catalyst consisting essentially of rhodium complexed with carbon monoxide and triphenylphosphine, said medium containing about 183 ppm rhodium (calculated as free metal) and whose catalytic activity had declined to about 40 percent of that of fresh catalyst, by shutting off the reactant feed gases, stopping the hydroformylation reaction and stripping essentially all (more than 99.5%) of said reactant gases from the reaction vessel and cycle lines.
• hydroformylation reaction medium so obtained showed it to contain about 22 percent by weight of butyraldehyde products, about 65 percent by weight of higher boiling aldehyde condensation by-products, about 0.3 percent by weight of free propyldiphenylphosphine, and about 11 percent by weight of free triphenylphosphine, the remainder consisting essentially of said rhodium complex catalyst, triphenylphosphine oxide and higher boiling organic components, e.g. aldehyde pentamers.
• Said derived hydroformylation reaction medium was then oxygenated while present in the same reaction vessel by passing a gaseous air-nitrogen mixture (about 4% oxygen) through said medium for about 13 hours, at about 60° to 67° C., about 60 p.s.i.g., and at an average feed flow rate of about 13.2 standard cubic feet of gas per hour per gallon of said derived medium to obtain an oxygenated treated hydroformylation reaction medium containing about 16 percent by weight of butyraldehyde products, about 0.08 percent by weight of free propyldiphenylphosphine and about 8 percent by weight of free triphenylphosphine, in addition to the other components mentioned above and present in said medium before said oxygen treatment.
• a gaseous air-nitrogen mixture about 4% oxygen
• Said analysis indicates that about 74 percent by weight of the original free propyldiphenylphosphine was oxidized to its corresponding phosphine oxide while only about 20 percent by weight of the original free triphenylphosphine was oxidized to its corresponding phosphine oxide by said oxygen treatment.
• a hydroformylation reaction medium was obtained from a continuous gaseous hydroformylation reaction of propylene to produce butyraldehyde, said reaction comprising feeding propylene, carbon monoxide and hydrogen to a reaction vessel and reacting same in the presence of a hydroformylation reaction medium contained therein comprising butyraldehyde products, higher boiling aldehyde condensation by-products as the solvent, free propyldiphenylphosphine, free triphenylphosphine, and a soluble rhodium complex hydroformylation catalyst consisting essentially of rhodium complexed with carbon monoxide and triphenylphosphine, said medium containing about 234 ppm rhodium (calculated as free metal) and whose catalytic activity had declined to about 40 percent of that of fresh catalyst, by shutting off the reactant feed gases, stopping the hydroformylation reaction and stripping essentially all (more than 99.5%) of said reactant gases from the reaction vessel and cycle lines.
• hydroformylation reaction medium so obtained showed it to contain about 24 percent by weight of butyraldehyde products, about 62 percent by weight of higher boiling aldehyde condensation by-products, about 0.3 percent by weight of free propyldiphenylphosphine, and about 13 percent by weight of free triphenylphosphine, the remainder consisting essentially of said rhodium complex catalyst, triphenylphosphine oxide and higher boiling organic components, e.g. aldehyde pentamers.
• Said derived hydroformylation reaction medium was then oxygenated while present in the same reaction vessel by passing a gaseous air-nitrogen mixture (about 4% oxygen) through said medium for about 13 hours, at about 54° to 65° C., about 60 p.s.i.g., and at an average feed flow rate of about 14.5 standard cubic feet of gas per hour per gallon of said derived medium to obtain an oxygenated treated hydroformylation reaction medium containing about 16 percent by weight of butyraldehyde products, about 0.1 percent by weight of free propyldiphenylphosphine and about 10 percent by weight of free triphenylphosphine, in addition to the other components mentioned above and present in said medium before said oxygen treatment.
• a gaseous air-nitrogen mixture about 4% oxygen
• Said analysis indicates that about 65 percent by weight of the original free propyldiphenyl phosphine was oxidized to its corresponding phosphine oxide while only about 11 percent by weight of the original free triphenylphosphine was oxidized to its corresponding phosphine oxide by said oxygen treatment.
• a hydroformylation reaction medium was obtained from a continuous gaseous hydroformylation reaction of propylene to produce butyraldehyde, said reaction comprising feeding propylene, carbon monoxide and hydrogen to a reaction vessel and reacting same in the presence of a hydroformylation reaction medium contained therein comprising butyraldehyde products, higher boiling aldehyde condensation by-products as the solvent, free propyldiphenylphosphine, free triphenylphosphine, and a soluble rhodium complex hydroformylation catalyst consisting essentially of rhodium complexed with carbon monoxide and triphenylphosphine, said medium containing about 267 ppm rhodium (calculated as free metal) and whose catalytic activity had declined to about 40 percent of that of fresh catalyst, by shutting off the reactant feed gases, stopping the hydroformylation reaction and stripping essentially all (more than 99.5%) of said reactant gases from the reaction vessel and cycle lines.
• hydroformylation reaction medium so obtained showed it to contain about 25 percent by weight of butyraldehyde products, about 60 percent by weight of higher boiling aldehyde condensation by-products, about 0.4 percent by weight of free propyldiphenylphosphine, and about 14 percent by weight of free triphenylphosphine, the remainder consisting essentially of said rhodium complex catalyst, triphenylphosphine oxide and higher boiling organic components, e.g. aldehyde pentamers.
• Said derived hydroformylation reaction medium was then oxygenated while present in the same reaction vessel by passing a gaseous air-nitrogen mixture (about 4% oxygen) through said medium for about 13 hours, at about 54° to 60° C., about 60 p.s.i.g., and at an average feed flow rate of about 14.7 standard cubic feet of gas per hour per gallon of said derived medium to obtain an oxygenated treated hydroformylation reaction medium containing about 16 percent by weight of butyraldehyde products, about 0.1 percent by weight of free propyldiphenyl phosphine and about 11 percent by weight of free triphenylphosphine, in addition to the other components mentioned above and present in said medium before said oxygen treatment.
• a gaseous air-nitrogen mixture about 4% oxygen
• Said analysis indicates that about 63 percent by weight of the original free propyldiphenylphosphine was oxidized to its corresponding phosphine oxide while only about 11 percent by weight of the original free triphenylphosphine was oxidized to its corresponding phosphine oxide by said oxygen treatment.

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